Process for the single stage manufacture of methyl isobutyl ketone



Unite State Pat O" 1 3,405,178 PROCESS FOR THE SINGLE STAGE MANUFAC- TURE OF'METHYL ISOBUTYL KETONE Johannes Wiillner, Kapellen Kreis Moers, and Friedrich i Engelhardt, Homberg (Lower Rhine), Germany, assignors ,to Rheinpreussen Aktiengesellschaft fiir Bergbau und Chemie, Homberg (Lower Rhine), Germany, a corporation of Germany No Drawing. Filed Mar. 2, 1964, Ser. No. 348,883

Claims priority, applicatiggl (liegrrnany, June 29, 1963,

"' 21 Claims. (Cl.260593) ABSTRACT OF THE DISCLOSURE Single stage process for producing methyl isobutyl ketone from acetone by liquid phase contact of acetone with hydrogenin the simultaneous presence of an acid cation exchange resin and a hydrogenation catalyst, e.g., palladium on carbon, optionally using a fixed bed or suspension catalyst system and concomitantly a batch or continuous technique, e.g.,'at temperatures between about S 0.200," -C, and pressures between about 1-50 atmospher'es absolute, with; a hy-drogen partial pressure between about 1.1, 25 atmospheres absolute. I

The present invention relates to a process for the single stage manufacture-of methyl'isobutyl ketone, and more particularly to'the production of methyl isobutyl ketone by contactin'g' 'acetone in liquid phase with hydrogen in the presence of an acid cation exchanger and a hydrogenationcatalystfi Various methodsare-known for the manufacture of methyl isobutyl ketone wherein-both liquid phase and vapor phase operations may be utilized. Most of the processes heretofore known for producing methyl isobutyl ketone have-been multistage processes. a

- In one three-stage process for the manufacture of methyl-isobutyl ketone, acetone is first made to react in thepresenc'e ofbasic condensation agents to form diacetone alcohoL which is then'dehydr'ated to mesityl oxide. In an additional stage, "the selective hydrogenation of the mesityl' oxide-take's place to form the methyl isobutyl ketone.

In a two-stage process for the manufacture of methyl isobutyl ketone, acetone is made to react in liquid phase, by "means of a strongly acid cation exchange resin, directly toformmesityl oxide, which is then separately hy- 'droge'nated to methyl isobutyl ketone-in a second stage. 1 I It is furthermore within the prior art to produce methyl isobutyl ketone-by a two-stage vapor phase method in which acetone vapor is passed over a solid catalyst such as lead acetate, resultingin the formation of mesityl oxide. The subsequent hydrogenation *by-means of a selectively operating catalyst leads to thedesired'methyl isobutyl ketone. 1 I

In German Patent 1,063,592 a process is disclosed which leads in a'single process stage from isopropyl al cohol to mixtures of methylisobutyl ketone and diisobutyl ketone. This'is a vapor-phase process in which the combined foim'a'tion'o'f methyl isobutyl ketone and diisobutyl ketonetakes place 'over a' mixed catalyst of copper oxide, magnesium oxide and pumice powder/Dis- 3,405,178 Patented Oct. 8, 1968 advantages of this process include a very low space-time yield amounting, according to the patent, to approximately 30 grams of methyl isobutyl ketone per liter of catalyst volume per hour.

The other processes mentioned above all require a relatively long operating time and relatively high apparatus expense. Furthermore, the space-time yield is slight or low, especially in the above-noted vapor-phase processes. Also, they result in a considerable production of by-products.

It is an object of the present invention to overcome the foregoing drawback and to provide a convenient, inexpensive, and versatile process for the single-stage production of methyl isobutyl ketone leading to good spacetime yields.

It is another object of the present invention to provide a process of the foregoing type utilizing a catalyst material under process conditions at which no gumming up or poisoning of the active catalyst surface takes place.

It is still another object of the present invention to provide a process of the foregoing type in whichv methyl isobutyl ketone is directly produced without appreciable formation of byproducts in spite of the use of a multiple component system for carrying out the reaction.

It is another object of the present invention to provide a process of the foregoing type in which the various re action steps take place simultaneously with the acetone being in liquid phase.

It is another object of the present invention to provide such a process as hereinabove described utilizing, simultaneously with a hydrogenation catalyst capable of 'selectively hydrogenating olefinic double bonds, a cation exchange component.

It is a further object of the present invention to provide a process which may be carried out either batchwise or continuously, preferably With agitation of the cation exchange component and the catalyst in the liquid phase of the reaction mixture.

It is a particular object of the present invention to utilize a strongly acid cation exchange resin as the cation exchange component which possesses good temperature resistance.

It is another object of the present invention to provide a process of the foregoing type in which a low hydrogen partial pressure, relative to the total pressure of the system, is employed to inhibit the formation of isopropylalcohol by the undesired hydrogenation of the acetone.

Other and further objects of the present invention will become apparent from a study of the within specification and accompanying examples.

It has been found in accordance with the present invention that a versatile single stage process for the production of methyl isobutyl ketone may be provided which comprises contacting acetone in liquid phase with hydrogen in the presence of an acid cation exchanger and an olefinic double bond selectively hydrogenating catalyst at elevated temperature, whereupon the methyl isobutyl ketone-containing reaction mixture may be recovered, and in turn the methyl isobutyl ketone itself as desired. The methyl isobutyl ketone is recovered preferably from the reaction mixture by distillation, and usually this takes place after the reaction mixture has been separated from the acid cation exchanger and the hydrogenation catalyst.

It will be appreciated that the instant process may be carried out batchwise or continuously. The solid or fixed bed embodiment or the suspension method with respect to the exchange resin can be used for the continuous process advantageously. For batch operation, it is preferable to use the suspension method. The process is usually effected at a temperature between about 50200 C. Elevated pressure may also be employed, such as a pressure between about 1-50 atmospheres absolute, with the partial pressure of the hydrogen present preferably ranging between about 1.125 atmospheres absolute.

The hydrogenation catalyst is significantly an olefinic bond-selectively hydrogenating catalyst such as metal selected from the group consisting of palladium, platinum, ruthenium, Raney nickel,'and Raney copper. The catalyst may be situated in divided form on a carrier support such as a carrier support selected from the group consisting of activated carbon, activated aluminum oxide, kieselguhr and pumice. k

In this connection, the cation exchanger is significantly a resin containing acid group and is generally selected from the group consisting of copolymers of monofunctional polymerizable compounds, and difunctional or polyfunctional polymerizable compounds having more than two functional groups, phenolic condensation resins which are obtained from phenols and/or their substitution products and aldehydes and/ or ketones.

The advantages of the present invention are surprising in many ways, and could not be foreseen, since there was no way to predict that no mutual inactivation would occur in the simultaneous presence of the two different activating components or catalysts including specifically the hydrogenation catalyst selectively acting on C=C double bonds and an acid cation exchange substance in admixture.

Also the fact that no objectionable resin formation occurs in the process of the invention, and hence no gumming up of the surfaces of the catalysts, is all the more surprising inasmuch as, according to experience, and by way of comparison, when mesityl oxide is formed from acetone over an acid cation exchange substance in the absence of hydrogen and of a selectively working hydrogenation catalyst, there develops a considerable amount of the more highly condensed byproducts-the so-called acetone oil and tarry byproductswhich settle in part on the surface of the catalyst. More surprising than anything else, however, is the possibility of now attaining the direct production of methyl isobutyl ketone without appreciable formation of byproducts, which is quiteunusual when it is considered that such a multiple-component system is present, as well as a plurality of reaction steps which take place simultaneously.

The quantity and distribution of the cation exchange component in the system is extraordinarily important as a factor governing the speed of the reaction. In addition to an optimum quantity of the cation exchange material corresponding to the prevailing conditions, another important factor especially in batch operation is the fineness of the grain, so as to have an optimum distribution in the reaction chamber through agitation.

Resins on a polymerization or condensation basis, containing sulfonic acid groups and/ or carboxylic acid groups, phosphonic acid groups or arsonic acid groups, are generally suitable. Cation exchangers on a polymerization basis include copolymers of monofunctional polymerizable compounds, such as styrene, mand p-methyl and -ethylstyrene, vinyl naphthalene, acrylic acid or methacrylic acid, and difunctional or polyfunctional compounds, such as divinyl benzenes, divinyl sulfone, ethylene dimethacrylate, divinyl ketone, vinyl maleate, vinyl esters of acrylic acid, inethacrylic acid, ethacrylic acid, divinyl esters of dibasic acids such as oxalic acid, maleic acid, etc. Suitable condensation type cation exchangers, on the other hand, include phenolic resins which are obtained from phenols and/or their substitution products and aldehydes and/or ketones. The manufacture of the cation exchange resins, which does not form an object of the present application, has been described in US. Patents Nos. 2,597,-

and the oerhi'afi Patents Nos. 960,858, 965,166, 1,031,513, 1,057,338, 755,119, 734,279, 749,553, 733,679, 747,644, 871,964, 914,186 and 919,666. The cation exchange resins are commercially available in the form of their alkali salts. These products can be converted to the acid form by treating the resin with a mineral acid, such as hydrochloric acid, and subsequently removing the excess mineral acid and the inorganic salt by washing with water.

It has proven particularlyadvantageous furthermore to use for the process of the invention strongly acid cation exchangers having good temperature resistance. Such temperature-resistant'.cation exchangers include polystyrene; divinyl benzene resinszcontaining,sulfonic, acid: groups, such as Dowex W-X8 of the Dow Chemical'Company, Midland, Mich., U.S.A.; Amberlite IR-llZ and .1 20 of the Rohm & Haas Company, Philadelphia, Pa.,;U.'S.'A.; Permutit RS of the Permutit A. G., Ber'lin-S chmargendorf, Berlin; Duolite C 25 of the Chemical Process Company, Redwood City, Calif., U. S.A and phenolic resins containing sulfonic acid groups, such as'Duolite"C"3 of the Chemical Process Company, Redwood City, Calif., USA; Lewatit PN and KSN of the Farbenfabriken Bayer, Leverkusen, Federal Republic of Germany, and Wofatit F, P and D of the VEB Earbenfabriken Wolfen, Germany. Mixtures of various types of cation exchangers may be used.

The acid cation exchange resins are especially'active when they are used in the water-free state. The presence of water decreases the' catalytic activity of the-resin;

One method of dehydration is drying at elevated temperatures under reduced pressure until a constantweight is obtained. Thus drying at C. up to about C. at a pressure of 5 to 10 mm. Hg will effect dehydration. The resin may also be dehydrated by azeotropic distillation with an organic liquid, such as an aromatic or aliphatic hydrocarbon until no further water is obtained in the distillate. Suitable hydrocarbons are heptane, isooctane, toluene, xylene or mixtures thereof. v

Appropriate hydrogenation catalysts usable in accordance with the present invention, as aforesaid, are, forexample, palladium, platinum, ruthenium, Raney nickel and Raney copper, which may be deposited in pieces or ,in finely divided form on catalyst supports such as, activated carbon (charcoal), activated aluminum oxide (alumina), kieselguhr and pumice, etc. W p

The process of the invention as mentioned above can be preformed both in batches and continuously. Specifically, for batch operation, use is expediently made of an appropriate stirring mechanism by which a thorough intermixing of all the reactants can be achieved.,Agitating mechanisms which operateaccording to the so-called typhoon principle have proven very appropriate (cf. Ullmann, Enzyclopadie der technischen Chemie, .2nd ed., vol. VII, 626 (Taifun), Verlag Urban & Schwarzenberg, Berlin, 1931).

The suspension or fixed bed process systems both can be utilized advantageously for the continuous method of operation. In the suspension process, the catalyst is-kept in a floating state by a suitable agitating mechanism. The acetone is fed in continuously and-the reaction product is continuously withdrawn from the reaction mixture. For the performance of the continuous process in the presence of a fixedly disposed catalyst, one may make vuse,- f0r example, of a vertical reaction tubethrough .which acetone is sprinkled downwardly over the mixtureof-the-two catalysts in the form of a fixed bed catalyst,v and through which hydrogen is fed from the bottom to the top inla countercurrent direction to the acetone, I

Notably, in the suspensionprocess, the quantity of the cation exchanger amounts to, ab out 5 to 1 00 parts by weight, preferably about 20 'to 50 partsby weight, pe r 100 parts by weight of liqu id'acetonepassing. throughl iit. While the amount of thecation exchanger prcsentsho'uld be relatively large, even relativelysmall.amountsiofhyr drogenation catalyst will suflice, say abo ut 0.01 to parts byweightof metal;peri 100 partsby weight ofacetone In the case' -of the.fixedlydisposedzcatalyst, on the other-hand, about 0.2 to 40 parts by weight and preferably about '1' to .10parts by weight of liquid acetone may be passed per hour through the .reaction chamber.for each part by weight of cation exchanger. The quantity of hydrogenation catalyst inthis instance amounts to about 0.0001 to. 1 part by weight, preferably about 0.0002 to 0.4 part by weightof metal, for each part by weight of cation exchanger used. Whena palladium catalyst is used, 0.0001 to 0.002=part by weight of .palladium metal with reference to each part by weight of cation exchanger used has proven sufficient in this connection.

: The ratio of moles of hydrogen per mole of acetone may vary from 0.121 to -5 :1. A preferred ratio is from 0.5:1to.2.5:1.* Significantly, according to the present invention, the partial pressure of the hydrogen should be kept low to prevent the formation of isopropyl alcohol by the undesired hydrogenation of the acetone. A hydrogen partial pressure of about 1.1 to 25 atm., preferably from about 1.5 to 15 atm., is entirely sufiicient for the thorough hydrogenation of C-,-C double, bonds. The inherent pressure of the system, of course, is governed by the particular composition of the reaction mixture and the temperature utilized.

The overall reaction takes place preferably at elevated temperatures as aforesaid. Whereas at 50 C. the speed i.

of reactionis, stillrelatively low,-substantiallyfaster conversion rates are achieved in the temperature range of 100 to 200 C. Temperatures ranging from 115 to 150 C.,. have provenespecially suitable. In any case, temperatures betweenabout 50 -200, C. are generally usable in accordance with the invention.

On account of the low hydrogen partial pressure used, the totalvapor pressure. of the system is to a greatextent determined; by the inherent Vapor pressure of the components at the reaction temperature and therefore the same maybe controlled as desired. In the 115-.-140 C. temperature range, for instance,-it is accordingly expedier 1 t to operate at total-pressures of about 3 to 20 atm., and preferably 6-15 atm., for optimum results, although total pressures evenhigherthan 20 atm. are also possible.

' p Example 1 v In a 2-liter1autoclave made of Remanit steel with a lifting-action agitator, a mixtureof 1 liter of acetone, 500 cc. of Dow'ex 50W-X8 in the hydrogen ion form, and 20 grams of 10% palladium charcoal, is heated with agitation ata partial pressure of 2.5 atm. hydrogen. At 75C., the beginning of theabsorption of hydrogen is noted,"wh'ich becomes increasingly rapid as the temperature further increases,, andreaches its peak at 130 C. after about 1 nonmagnynne retaining 10 atm. of total pressure fa'rid keeping" thel temper'ature at" 130 C., the mixture is agitated"for: another 4 hours while constantly adding 'hydrogen.asjneeded. After c'ooling, the reaction mixture is filtered free of catalysti It shows a methyl isobutyl ketone'content"of"44;9%" by weight. Through the colummdistillatio'n of-722 grams of the filtered reaction mixture, "283 grams of methyl isobutyl ketone are obtained, which pass over in-the boiling range of 114- 117'..c- I a In the following comparisonexperiment, acetone is in themanner as described in Example 1 contacted with an acid cation exchange resin-in the absence both of, hydrogen and a hydrogenating catalyst, whereby mesityl oxide i f r a a; A mixture of l liter of acetone and 500 cc. of Dowex sow-x8 in the hydrogen ion form is heated with agitaltion1to130 C. After lhours, the mixture is cooled and filtered 'freeof catalyst. j'Ihe filtered reaction product exhibits 6.7% by'weightlof mesityl oxide, 86.4% by weight of unreacted acetone, 4;2%"by Weight of water and 5.7%

V --..;'6:. byweight of higher ketones. The rest contains undefinable products. The catalyst used soon becomes deactivated. This comparison example shows the superiority of the joint utilisation of a cation exchanger and a hydrogenation catalyst. i e Example 2 'In accordance with the procedure described in Example 1',"700'cc. of acetone, 700 cc. of cation exchange resin Dowex 50W-X8 in the hydrogen ion form, and 15 g. of 10% palladium charcoal are heated with agitation to 130" C., and a pressure of 10 atm. is maintained by feeding in hydrogen as required. After 3 /2 hours of operating time, the experiment is interrupted. The filtered reaction product exhibits a methyl isobutyl ketone content of 57.3% by weight.

Example 3 700 cc. of acetone, 700 cc. of Dowex 50W-X8 cation exchange resin in the hydrogen ion form and 15 grams of 10% weight palladium charcoal are heated in accordance with the procedure described in Example 2, to 145 C., with agitation. The hydrogen pressure is adjusted to the higher inherent vapor pressure of the system so that a total pressure of 16 atm. is produced. After 5 hours of operating time, the hydrogen absorption has become so slow that the experiment is broken off. The filtered reaction product exhibits a methyl isobutyl ketone content of 70.0% by weight.

' Example 4 700 cc. of acetone are treated with hydrogen in accordance with the procedure described in Example 1, in the presence, of 2 00 g. of Amberlite IR-1l2 cation exchange resin the hydrogen ion form previously .vacuum dried at C., and of 15 g. of 10% palladium charcoal, at C., with agitation, so that a total pressure of 11.5 atm. is established. After 3 /2 hours of operating time, the reaction mixture shows a content of 68.9% by weight methyl isobutyl ketone.

Example 5 In the manner described in Example 1, 1000 cc. of acetone, 500 cc. of Lewatit KSN cation exchange resin in the hydrogen ion form, and 20 g. of 2% ruthenium charcoal are heated with" agitation to C., and a pressure of 13 atm. is maintained by the feeding in of hydrogen as required. After 3 /2 hours of operating time, the experiment is discontinued. The filtered reaction product exhibits a 54.6% by weight content of methyl isobutyl ketone.

Example 6 In a 1.2-liter container having a pressure agitating mechanism with an agitating system working according to the typhoon principle, steam jacket healing and a built-in filter candle, a mixture of 588 g. of acetone, 232 g. of dried cation exchange resin Duolite C-3, in the hydrogen ion form and 20 g. of 2% palladium charcoal, are heated to 135 C. under a constant hydrogen partial pressure of 2 atm., by means of steam at 2.5 atmospheres excess pressure, and the reaction mixture is agitated for 1 hour without feeding in acetone. Then, the feeding of 392 g. of acetone per hour is begun, while at the same time 392 g. of reaction product per hour are removed through the filter candle. Over a period of 50 hours, a methyl isobutyl ketone content of 27% by weight develops in the mixture that is being drawn ofi.

Example 7 In a 2-liter Remanit steel autoclave with lifting-action agitation, a mixture of 750 cc. of acetone, 200 g. of dried cation exchange resin Permutite R5 in the hydrogen ion form and 50' g. of Raney nickel previously desiccated with acetone, is heated to 130-135 C. with agitation, while maintaining a hydrogen partial pressure of 5 atm. After continuing the agitation for 3 /2 hours under these reaction conditions, the mixture is allowed to cool under agitation, and a methyl isobutyl ketone content of 55.3%

by' weight is foundin the reactionrnixture upon filtering su'c'h mixture freeofcatalyst.

Example 8' The reaction tube used is a vertical stainless steel pressure tube of cm. diameter andv 1m. length and is heated with steam at a pressure of 2.5 atmospheric gage. Up to a level of .92 cm., the tube is.fill ed with 6 inrn. tablets obtained by pressmolding of a r'nixture of equal par,ts by weight of Dowex 50W-X8 and 5% palladium charcoal. The tube contains 1.8 liters of the fixed-bed catalyst as specified with a bulk density of 0:6. The weight of the catalyst is 1.08 kg. In this reaction tube, 1000 cc. of acetone are forced in per hour at the top, and 90 liters of hydrogen are forced in per hour at the bottom. The unreacted part of the hydrogen that passes through the catalyst column is taken off at the top and fed back to the reaction tube with fresh hydrogen by a gas circulation pump. In the reactor, where a temperature of 135 C. is produced as a result of the heating with 2.5 excess atmospheres of steam, a pressure of atmospheres is maintained by proportioning the hydrogen accordingly. In the reaction product drawn off at the bottom, the 'methyl isobutyl ketone content slowly increases, and then establishes itself at 35 weight percent of methyl isobutyl ketone.

Example 9 In a 2-liter Remanit steel autoclave with lifting-action agitating, a mixture of 750 cc. of acetone, 100 grams of dried cation exchange resin Dowex'50WX8 in the hydrogen ion form, 100 grams dried cation exchange resin Duolite C in the hydrogen ion form and 50 grams of Raney copper previously desiccated with acetone, is heated to 133l37 C. with agitation, while maintaining a hydrogen partial pressure of 6 atm. After continuing the agitation for 3 hours under these reaction conditions, the mixture is. allowed to cool under agitation, and a methyl isobutyl ketone content of 49.8% by weight is found in the reaction mixture upon filtering free of catalyst.

Example 10 In a 1.2 liter container having a pressure agitating mechanism with an agitating system working according to the typhoon principle, steam jacket heating and a builtin filter candle, amixture of 588' grams of acetone, 150 grams of dried cation exchange resin A'mberlite IR-1l 2 ,in the hydrogen ion form, 82 grams of dried cation exchange resin Permutite RS in the hydrogen ion form and 20 grams of 2% platinum charcoal, are heated to 140 C. under a constant hydrogen partial pressure of 2 at-m., by means of steam at 2.5 atmospheres excess pressure, and the reaction mixture is agitated for 1 hour without feeding in acetone. Then, the feeding of 392 grams of acetone per hour is begun, while at the same time 392 grams of reactionproduct per hour are removed through the filter candle. Over a period of 50 hours, a methyl isobutyl ketone content of 26% by weight develops in the mixture that is being drawn otf.

' What is claimed is:

1. Process for the single-stage production of methyl isobutyl ketone which comprises contacting acetone in liquid phase with hydrogen in the simultaneous presence of a strongly acid cation exchange resin in its acid form and an olefinic double bond selectively hydrogenating catalyst at an elevated temperature between about 50200 C. and an elevated pressure between about l-50 atmospheres absolute, and recovering the methyl isobutyl ketone-containing reaction mixture.

I 2. Process according to claim 1 wherein the methyl isobutyl ketone is recovered from the reaction mixture.

3. Process according to ,claim 1 wherein the process is carriedout batchwise.

4. Process according to claim 1 wherein the process is carried out continuously.

5. Process according to claim 1 wherein the process is carried out in a suspension catalyst system using the:cat+ ion' exchange resin in an amount between about S-IOO parts by weight per parts by weight of acetone pr'esend andsaid hydrogenation catalyst in an .amQunt between about 0.01-5 parts by weight of metal per -'100 parts by weight of acetone present. W f

6. Process according'to claim 1 wherein the processis carried out in a fixed=bed catalyst system, and' 0;2-40 parts'by -weight of acetone per hour are used 'per part by weight of cation-exchange resin present, vsaid hydrogenation catalyst being present in an amount between about 020001 to l part by Weight of metal per part by weight of cation exchange .resin present. A 1

7. Process according to claim 6, wherein 1 to 10 parts by weight of acetone are used per hour per part'by weight of cation exchange resin present, said hydrogenation catalyst being present in an amount between 0.0002 to 0.4 part by weight of metal per part by Weightof cation exchange present.

8. Process according to claim 7, wherein a palladium catalyst is used as hydrogenation catalyst in an amount between 0.0001 to 0.0002 part by weight of metal per part by weight of cation exchange resin present.

9. Process according to claim 1 wherein the process-is carried out at a temperature between about 100-200 C.

10. Process according to claim 9, wherein the'process is carried out at a temperature between about to 150 C. l

11. Process accordingto claim 1 wherein the process is carried out at a temperature between about'115 to C. and at an elevated pressure between about 3 to-20 atmospheres absolute. v

12. Process according to claim 11 wherein the partial pressure of the hydrogen present ranges between about 1.1-25 atmospheres absolute. t

13. Process according to claim 12, wherein said pressure is between about 6-l5 atmospheres absolute,with the partial pressure of the hydrogen-presentrangingbetween about 1.5 to 15' atmospheres absolute. I t

14. Process according to claim 1 wherein-said hydrogenation catalyst is selected from the group consisting of palladium, platinum, ruthenium, Raney nickel and Raney copper. 1

15. Process according to claim 14whereinsaid catalyst is situated in divided form on acarrier support.

16. Process according to claim 15 wherein said carrier support is selected from the group consisting of activated carbon, activated aluminum oxide, kiselguhr and pumice. I I

17. Process according to claim l'whe'rein said cation exchange resin is used in the water-free state.

18. Process according to claim 1, wherein mixtures of cation'exchange resins are'used. ii i 19. In the process for the. manufacture of methyl isobutyl ketone in a single stage, the limpr'ovement which comprises contacting acetone in liquid" phase with hydrogen in gaseous phase inthe pre'sence 'o'f a mixture bf a strongly acid cation exchange resin" in its'acid form with a hydrogenation catalyst for-selectively hydrogenating ole finic doublebondswhich is selectedjrom the groupcon sisting of palladium, platinum, ruthenium, Raney.-nickel and Raney copper, at a temperature between about, 50-.- 200 C. and a total pressure between about 1-50 atmospheres absolute, with' the "partial 'pressure of the:hydrogen present ranging btween -:1.125 atmospheres abso' lute, and recovering the methyl isobutyl ketone-formed from the reaction mixture. 7 i

20. Improvement according to claim 19 whereiirthe process is carried out irra-suspensioncatalyst system, said cation exchange resin being pfesent'in'ari amoiint between about 5-100 parts by wightper 100 parts" 'byiwe' ghtlo f liquid acetone present, ahdls'aidhydrogehati on catalyst being present in anarnount'bet wen parts by weight of metal per 100 parts by weight of liquid acetone References Cited present. I

21. Improvement according to claim 18 wherein the UN TED T PATENTS process is carried out in a fixed bed catalyst system, said 2,499,172 2/1950 f 260 593 acetone being added to the reaction mixture in liquid form 5 2,367,078 1/1945 Welzmann 260 593 at a rate between about 0.2-40 parts by weight per hour per part by weight of said cation exchange resin, and said OTHER REFERENCES hydrogenation catalyst being present in an amount be- Klein et al.: Ind. Eng. Chem. 48, 1278-1286 (1956).

tween about 0.0001-1 part by weight of metal per part y weight of cation exchange resin present 10 DANIEL D. HORWITZ, Primary Examiner. 

